Sorbents for the oxidation and removal of mercury

ABSTRACT

A promoted activated carbon sorbent is described that is highly effective for the removal of mercury from flue gas streams. The sorbent comprises a new modified carbon form containing reactive forms of halogen and halides. Optional components may be added to increase reactivity and mercury capacity. These may be added directly with the sorbent, or to the flue gas to enhance sorbent performance and/or mercury capture. Mercury removal efficiencies obtained exceed conventional methods. The sorbent can be regenerated and reused. Sorbent treatment and preparation methods are also described. New methods for in-flight preparation, introduction, and control of the active sorbent into the mercury contaminated gas stream are described.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a divisional of U.S. patent application Ser. No.11/209,163 filed Aug. 22, 2005, entitled “Sorbents for the Oxidation andRemoval of Mercury”, which claims the benefit of U.S. ProvisionalApplication Ser. No. 60/605,640, filed Aug. 30, 2004, both applicationsare hereby incorporated herein by reference in their entirety for allpurposes.

STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT

This invention was made with United States Government support underGrant Numbers R 827649-01 and CR 830929-01 awarded by the United StatesEnvironmental Protection Agency and under Contract NumberDE-FC26-98FT40320 awarded by the United States Department of Energy. TheUnited States Government has certain rights in this invention.

BACKGROUND OF THE INVENTION

1. Technical Field of the Invention

The present invention relates to methods and materials for the removalof pollutants from flue gas or product gas from a gasification system.In particular, mercury is removed from gas streams generated during theburning or gasification of fossil fuels by highly reactive regenerablesorbents.

2. BACKGROUND OF THE INVENTION

The combustion and gasification of fossil fuel such as coal generatesflue gas that contains mercury and other trace elements that originatefrom the fuel. The release of the mercury (and other pollutants) to theenvironment must be controlled by use of sorbents, scrubbers, filters,precipitators, and other removal technologies. Mercury is initiallypresent in the elemental form during combustion and gasification. Indownstream process sections, such as in the ducts and stack of acombustion system, some of the elemental mercury is oxidized. The amountthat is oxidized depends on the amount of acid gases present in the fluegas and other factors. Amounts of mercury vary with the fuel, butconcentrations of mercury in the stream of flue gas from coal combustionare typically less than 5 parts per billion (ppb). Large coal combustionfacilities such as electric utilities may emit a pound of mercury, ormore, per day. Mercury removal applications include, without limitation,flue gas from coal (or other fossil fuel) combustion, wasteincineration, product gas from gasification, as well as off gases frommineral processing, metal refining, retorting, cement manufacturing,chloralkali plants, dental facilities, and crematories.

Mercury Sorbent Technologies

Several types of mercury control methods for flue gas have beeninvestigated, including injection of fine sorbent particles into a fluegas duct and passing the flue gas through a sorbent bed. Fine-particleinjection sorbents include activated carbon, metal oxide sorbent, sodiumsulfide particles, and basic silicate or oxide sorbents. When particleinjection is employed, the mercury captured on the sorbent particles isremoved from the gas stream in a bag house or electrostatic precipitator(ESP) and collected along with ash particulate. The sulfide and basicsilicate and oxide particles are effective only for the oxidizedmercury, and the metal oxide sorbents exhibit slower capture kineticsthan the carbon particles. Additionally, injection of fine carbonparticles into the flue gas stream has been only partially successful inremoving mercury, especially elemental mercury, where effective removalof only about 60% is attained for some applications with a FF (fabricfilter) to collect carbon and ash. Even lower removal rates have beenobserved when using an ESP to collect the carbon because the contacttime of the carbon with the gas is very short.

A major problem with existing carbon injection systems is that thesorbent is initially unreactive, and only after extended exposure to theflue gas does the sorbent become effectively seasoned and provideincreased reactivity with the mercury in the gas. Consequently, thesesorbents must be used in large amounts, at high sorbent-to-mercuryratios, to effectively capture the mercury. These sorbents tend to berelatively expensive and cannot be easily separated from the ash forregeneration and reuse. The collection of carbon in the ash also createssolid waste disposal problems, and the spent sorbent may contaminate thecollected ash, preventing its use in various applications.

Accordingly, there remains a need for more economical and effectivemercury removal technology. This invention provides for cost-effectiveremoval of pollutants including mercury, using sorbent enhancementadditives and/or highly reactive sorbents, with contact times of seconds(or less), and that may be regenerated and reused.

SUMMARY

It is thus an object of the present invention to overcome thedeficiencies of the prior art and thereby to provide new and economicalmethods for the removal of mercury from the gases produced in theutilization of fossil fuels.

A halogen/halide promoted activated carbon sorbent is described that ishighly effective for the removal of mercury from flue gas streams. Thesorbent comprises a new halide-modified carbon form containing areactive compound produced by the reaction of bromine (or halide orother halogen) with the carbon. Optional secondary components and alkalimay be added to further increase reactivity and mercury capacity.Mercury removal efficiencies obtained exceed or match conventionalmethods with added benefits such as reduced costs. Optionally, thesorbent can be regenerated and reused. Sorbent treatment and/orpreparation methods are also described. New methods for in-flightpreparation, introduction, and control of the active sorbent into themercury contaminated gas stream are described.

In some embodiments, a promoted carbon sorbent is provided comprising abase activated carbon that has reacted with a promoter selected from thegroup consisting of halides, halogens, and combinations thereof, suchthat the reaction product is effective for the removal of mercury from agas stream.

In an embodiment, a promoted carbon sorbent is provided wherein the baseactivated carbon is selected from the group consisting of powderedactivated carbon, granular activated carbon, carbon black, carbon fiber,aerogel carbon, pyrolysis char, activated carbon with an averageparticle size greater than that of flyash produced such that it isphysically separable therefrom, and combinations thereof, and thepromoter is selected from the group consisting of molecular halogens,Group V (CAS nomenclature is used throughout) halides, Group VI halides,hydrohalides, and combinations thereof. In an embodiment, the baseactivated carbon may have a mass mean particle diameter such that it canbe substantially separated by physical means from entrained ash in thegas stream from which mercury is to be removed. In an embodiment, thebase activated carbon may have a mass mean particle diameter greaterthan about 40 micrometers.

In another embodiment, the sorbent comprises from about 1 to about 30grams promoter per 100 grams of base activated carbon. Anotherembodiment further comprises an optional secondary component comprisinga halogen or a hydrohalide such that the reactivity and mercury capacityof the sorbent are enhanced.

In another embodiment, the concentration of the optional secondarycomponent on the finished sorbent is within the range of from about 1 toabout 15 wt-% of the concentration of the promoter on the finishedsorbent.

In another embodiment, an optional alkali component may preferably beadded to provide a synergistic effect through combination of this alkaliwith the primary sorbent.

In another embodiment, the optional secondary component is selected fromthe group consisting of Group V halides, Group VI halides, HI, HBr, HCl,and combinations thereof. In another embodiment, the promoter issubstantially in vapor form when combined with the base activatedcarbon. In another embodiment, the promoter is combined with an organicsolvent prior to reaction with the base activated carbon. In anotherembodiment, the promoter and optional secondary component are combinedwith the base activated carbon substantially simultaneously. Anotherembodiment further comprises adding a mercury-stabilizing reagentselected from the group consisting of S, Se, H₂S, SO₂, H₂Se, SeO₂, CS₂,P₂S₅, and combinations thereof. Another embodiment further comprisesadding an optional alkali component.

In an embodiment, a method is provided comprising providing a granularactivated carbon; reacting the activated carbon with a promoter selectedfrom the group consisting of halogens, halides, and combinationsthereof, such that the reaction product comprises a promoted carbonsorbent effective for removal of mercury from a gas stream. In a furtherembodiment, the reaction product comprises from about 1 to about 30grams promoter per 100 grams activated carbon. In another embodiment thereaction product has an average particle size distribution greater thanthe average size of entrained ash particles in the gas stream from whichmercury is to be removed, such that the reaction product can besubstantially removed from the entrained ash particles by physicalmeans. In another embodiment the reaction product has a mass meanparticle diameter greater than about 40 micrometers.

In another embodiment, the promoter is selected from the groupconsisting of molecular halogens, hydrohalides, Group V halides, GroupVI halides, and combinations thereof. In another embodiment the promoteris in the gas phase when contacting the activated carbon. In anotherembodiment, the promoter is in an organic solvent when contacting theactivated carbon.

In another embodiment, the promoter is selected from the groupconsisting of Br₂, a Group V bromide, a Group VI bromide, andcombinations thereof.

In another embodiment, the method further comprises reacting thegranular activated carbon with an optional secondary componentcomprising a halogen or a hydrohalide such that the reactivity andmercury capacity of the sorbent are enhanced. In another embodiment, thepromoter and optional secondary component are contacted simultaneouslywith the activated carbon. In another embodiment the method furthercomprises adding a mercury-stabilizing reagent selected from the groupconsisting of S, Se, H₂S, SO₂, H₂Se, SeO₂, CS₂, P₂S₅, and combinationsthereof. In an embodiment, a method is provided for control of mercuryin a flue gas with substantially lower sorbent requirements. Throughenhanced sorbent reactivity, mercury removal per gram of sorbent isincrease, thereby decreasing the capital and operating costs bydecreasing sorbent requirements.

In an embodiment, a method is provided for reducing mercury in flue gascomprising providing a sorbent, injecting the sorbent into amercury-containing flue gas stream, collecting greater than 70 wt-% ofthe mercury in the flue gas on the sorbent to produce a cleaned fluegas, and substantially recovering the sorbent from the cleaned flue gas.In embodiments where less than 70 wt-% mercury removal is desired, therequired removal may preferably be attained using less than half as muchcarbon as would be required with standard (non-enhanced) carbon. In afurther embodiment, the method further comprises monitoring the mercurycontent of the clean flue gas, regenerating the recovered sorbent, andusing the monitored mercury content of the cleaned flue gas to controlthe rate of injection of the sorbent. In another embodiment the injectedsorbent is prepared in-flight by reacting an activated carbon and apromoter within a pneumatic transport line from which the reactionproduct is injected to the mercury-containing flue gas stream.

In another embodiment, the promoter is selected from the groupconsisting of molecular halogens, halides, and combinations thereof. Inanother embodiment, the promoter is reacted in the gas phase or as avapor. In another embodiment, the promoter is added at from about 1 toabout 30 grams per 100 grams of activated carbon.

In another embodiment, the injected sorbent is prepared in-flight byreacting an activated carbon, a promoter, and an optional secondarycomponent to enhance the reactivity and capacity of the sorbent within apneumatic transport line from which the reaction product is injected tothe mercury-containing flue gas stream.

In another embodiment, the optional secondary component is selected fromthe group consisting of iodine, hydrohalides, Group V halides, Group VIhalides, and combinations thereof. In another embodiment, the optionalsecondary component is added at from about 1 to about 15 wt-% of thepromoter content. In another embodiment, the method further comprisesadding to the sorbent a mercury-stabilizing reagent selected from thegroup consisting of S, Se, H₂S, SO₂, H₂Se, SeO₂, CS₂, P₂S₅, andcombinations thereof.

In an embodiment, the method further comprises co-injecting an optionalalkaline material, including without limitation alkaline and alkalineearth components, to improve the efficiency of mercury capture bycapturing oxidized mercury and/or capturing gaseous components thatmight otherwise reduce sorbent capacity. In another embodiment, theoptional alkaline material may preferably comprise calcium oxide, sodiumcarbonate, and the like, as are known in the art.

In another embodiment, the method further comprises using the monitoredmercury content of the cleaned flue gas to control the composition ofthe sorbent. In another embodiment, the injected sorbent is preparedin-flight by reacting an activated carbon and a promoter within apneumatic transport line from which the reaction product is injected tothe mercury-containing flue gas stream, wherein the promoter is selectedfrom the group consisting of molecular halogens, halides, andcombinations thereof, wherein the promoter is reacted in the gas phaseor as a vapor, wherein the promoter is added at from about 1 to about 30grams per 100 grams of activated carbon, wherein the rate at which thepromoter is added and the rate of sorbent injection are determined by adigital computer based at least in part on the monitored mercury contentof the cleaned flue gas.

In an embodiment, a method for reducing the mercury content of a mercuryand ash containing gas stream is provided wherein particulate activatedcarbon sorbent with a mass mean size greater than 40 μm is injected intothe gas stream, mercury is removed from the gas by the sorbentparticles, the sorbent particles are separated from the ash particles onthe basis of size, and the sorbent particles are re-injected to the gasstream. In another embodiment, the mercury-containing sorbent particlesare regenerated to remove some or substantially all of the mercury. Inanother embodiment, an alkaline component is co-injected into the gasstream. In another embodiment, the sorbent may further comprise apromoter. The promoter may preferably comprise a halide, a halogen, orboth.

As will be described in more detail below, the present invention thusprovides several advantages over previously known techniques, includingsignificantly more effective and economical mercury sorbents foreffluent gases, advantageously applicable to treating gas streams fromfired equipment and gasification systems.

The foregoing has outlined rather broadly the features and technicaladvantages of the present invention in order that the detaileddescription of the invention that follows may be better understood.Additional features and advantages of the invention will be describedhereinafter that form the subject of the claims of the invention. Itshould be appreciated by those skilled in the art that the conceptionand specific embodiments disclosed may be readily utilized as a basisfor modifying or designing other structures for carrying out the samepurposes of the present invention. It should also be realized by thoseskilled in the art that such equivalent constructions do not depart fromthe spirit and scope of the invention as set forth in the appendedclaims.

BRIEF DESCRIPTION OF THE DRAWINGS

For a more detailed description of the preferred embodiments of thepresent invention, reference will now be made to the accompanyingdrawings.

FIG. 1 schematically illustrates methods for preparation of promotedcarbon sorbents in accordance with the present invention.

FIG. 2 illustrates a proposed mechanistic model of the chemicalreactions resulting in the oxidation and capture of mercury.

FIG. 3 schematically illustrates preparation of promoted carbon sorbentsand processes for flue gas mercury reduction in flue gases and/orproduct gases from a gasification system in accordance with the presentinvention, including in-flight preparation of promoted carbon sorbent.

FIG. 4 is a diagram illustrating breakthrough curves for 5 wt/wt %brominated NORIT Darco FGD sorbent (37 mg+113 mg sand) in low-HCl (1ppm) synthetic flue gas.

FIG. 5 is a diagram illustrating breakthrough curves for non-halogenatedNORIT Darco FGD sorbent (37 mg+113 mg sand) in low-HCl (1 ppm) syntheticflue gas.

FIG. 6 is a bar chart illustrating pilot-scale mercury removal results,including large-size sorbent results.

FIG. 7 is a diagram illustrating the effects of sorbent size andinjection rate on mercury removal for ESPs and fabric filters.

FIG. 8 is a diagram illustrating the breakthrough curves for abrominated NORIT Darco FGD sorbent with inert sand.

FIG. 9 is a diagram illustrating the breakthrough curves for brominatedNORIT Darco FGD sorbent with a co-injected alkali material.

FIG. 10 is a plot of mercury removal vs. carbon injection rate with andwithout co-injection of alkali material.

DETAILED DESCRIPTION

Herein will be described in detail specific preferred embodiments of thepresent invention, with the understanding that the present disclosure isto be considered an exemplification of the principles of the invention,and is not intended to limit the invention to that illustrated anddescribed herein. The present invention is susceptible to preferredembodiments of different forms or order and should not be interpreted tobe limited to the specifically expressed methods or compositionscontained herein. In particular, various preferred embodiments of thepresent invention provide a number of different configurations andapplications of the inventive method, compositions, and their uses.

The present invention provides a cost-effective way to capturepollutants by utilizing exceptionally reactive halogen/halide promotedcarbon sorbents using a bromide (or other halogen/halide) treatment ofthe carbon, that capture mercury via mercury-sorbent surface reactions,at very short contact times of seconds or less. The sorbent does notrequire in situ activation (no induction period) in the gas stream toachieve high reactivity, as do conventional activated carbon sorbents.The reactivity of the sorbent toward the pollutants is greatly enhancedand the sorption capacity can be regenerated, the promoted sorbent maybe regenerated, recycled and/or reused.

The treated carbons, treatment techniques, and optional additivesdiscussed herein have applicability to mercury control from the productor effluent gas or gases from gasification systems, syngas generators,and other mercury-containing gas streams, in addition to the flue gasfrom combustion systems. Thus, it should be understood that the termscombustion system and flue gas as used throughout this description mayapply equally to gasification systems and syngas or fuel gas, as will beunderstood by those skilled in the art.

Referring now to FIG. 1, there is shown a block flow diagramillustrating some preferred embodiments of the process of the presentinvention to prepare promoted sorbents useful for mercury capture fromflue gas and/or product gas form a gasification system streams. In apreferred embodiment illustrated by path 10-20, block 10 illustratesproviding a base activated carbon, and adding a halogen or halidepromoter that reacts with the carbon, illustrated at block 20, toproduce a product promoted carbon sorbent. In embodiments where thehalogen or halide is added, for example, as a vapor, no further stepsmay be necessary. In embodiments where the halogen or halide is addedin, for example, a solvent, it may be desirable to employ solventremoval as illustrated by block 20A.

Referring still to FIG. 1, another preferred embodiment of the processof the present invention is illustrated by path 10-20-30, comprisingproviding a base activated carbon as shown by block 10, adding a halogenor halide promoter that reacts with the carbon, illustrated at block 20,and adding a secondary component illustrated at block 30 that reactswith the result of block 20 to produce a product promoted carbonsorbent. In embodiments where both the halogen or halide promoter andthe secondary component are added, for example, as a vapor, no furthersteps may be necessary. In embodiments where the halogen or halidepromoter and/or secondary component are added in, for example, asolvent, it may be desirable to employ solvent removal as illustrated byblock 30A.

Referring still to FIG. 1, another preferred embodiment of the processof the present invention is illustrated by path 10-40, comprisingproviding a base activated carbon as illustrated at block 10, and addinga halogen or halide promoter and a secondary component to the activatedcarbon together, with which they react as illustrated by block 40,producing a product promoted carbon sorbent. As above, in embodimentswhere vapor additions are made to the activated carbon no further stepsmay be desired. In embodiments where one or more components are added insolvent, a solvent removal step may be provided as illustrated by block40A.

Referring still to FIG. 1, also illustrated are preferred embodiments inwhich, as illustrated by block 50, a flue gas stream is treated withproduct promoted carbon sorbent prepared as described above.

In some preferred embodiments the activated carbon provided maypreferably be any of several types, as understood by those skilled inthe art. For example, the activated carbon may include powderedactivated carbon, granular activated carbon, carbon black, carbon fiber,carbon honeycomb or plate structure, aerogel carbon film, pyrolysischar, regenerated activated carbon from product promoted carbon sorbent,or other types as known in the art.

In some preferred embodiments the activated carbon provided maypreferably be any of several types, as understood by those skilled inthe art. For example, the activated carbon may include powderedactivated carbon, granular activated carbon, carbon black, carbon fiber,carbon honeycomb or plate structure, aerogel carbon film, pyrolysischar, an activated carbon or regenerated activated carbon with a massmean particle size greater than fly ash in a flue gas stream to betreated.

In some preferred embodiments the activated carbon provided maypreferably be any of several types, as understood by those skilled inthe art. For example, the activated carbon may include powderedactivated carbon, granular activated carbon, carbon black, carbon fiber,carbon honeycomb or plate structure, aerogel carbon film, pyrolysischar, an activated carbon or regenerated activated carbon with a massmean particle diameter preferably greater than 40 micrometers, morepreferably greater than 60 micrometers, or a particle size distributiongreater than that of the fly ash or entrained ash in a flue gas streamto be treated, such that the activated carbon and ash can be separatedby physical means.

In some preferred embodiments, the halogen or halide promoter that isadded to, and reacts with, the base activated carbon may preferablycomprise, by way of illustration and not limitation, a molecular halogenin vapor or gaseous form, a molecular halogen in an organic solvent, aGroup V or Group VI halide, such as PBr₃ or SCl₂, respectively, invapor, liquid, or solution form (though not in an aqueous solvent).

Embodiments are also provided in which the organic solvent maypreferably comprise a chlorinated hydrocarbon, such as dichloromethane,a hydrocarbon solvent, including for example, petroleum ether, ligroin,pentane, hexane, toluene, and benzene, carbon disulfide, a wastesolvent, an ether, a recycled solvent, a supercritical solvent, such assupercritical CO₂, water (though not in the case of a Group V or GroupVI halide), and others as will be apparent to those of skill in the art.

Referring now to FIG. 2, there is illustrated a theory developed fromscientific evidence to explain the nature of the promoting compounds.For example, as illustrated in FIG. 2, hydrogen bromide reacts with theunsaturated structure of the activated carbon. This may be, by way ofillustration only, a carbene species on the edge of the graphene sheetstructures of the carbon. Molecular bromine or a bromine compound reactsto form a similar structure, with a positive carbon that is active foroxidizing the mercury with subsequent capture by the sorbent.

It has now been found that the formation of the new bromide compoundwith carbon increases their reactivity toward mercury and otherpollutants. Additionally, the resulting bromide compound is uniquelysuited to facilitate oxidation of the mercury. The effectiveness of theoxidation apparently results from the promotion effect of the halide,exerted on the developing positive charge on the mercury during theoxidation, known in the chemical art as a specific catalytic effect.Thus, as the mercury electrons are drawn toward the positive carbon, thehalide anion electrons are pushing in from the other side, stabilizingthe positive charge developing on the mercury and lowering the energyrequirement for the oxidation process. Bromide is especially reactive,owing to the highly polarizable electrons in the outer 4 p orbitals ofthe ion. Thus, adding HBr or Br₂ to the carbon forms a similar carbonbromide, in which the positive carbon oxidizes the mercury with theassistance of the bromide ion.

Referring now to FIG. 3, a schematic flow diagram is provided of mercurycontrol system 100 comprising preparation of promoted carbon sorbents,and flue gas mercury reduction, in accordance with preferred embodimentsof the present invention. There is provided base activated carbonreservoir 110, an optional halogen/halide promoter reservoir 120, anoptional secondary component reservoir 130, and an optional akalicomponent reservoir 180, each of which with corresponding flow controldevice(s) 201, 202, 203, and 208/209, respectively. In conjunction withthe optional alkali component reservoir 180, optional flow controldevices 208 and 209 can be used independently, together, or not at all.

Reservoirs 110, 120, 130, and 180 connect through their respective flowcontrol devices and via associated piping, to transport line 115.Optional alkali component reservoir 180 may also connect, throughrespective flow control devices and via associated piping, to transportline 118. A source of air, nitrogen, or other transport gas(es) isprovided by gas source 170 to transport line 115 for the purpose ofentraining materials discharged from reservoirs 110, 120, 130, and 180and injecting such materials, via injection point 116, into contaminatedflue gas stream 15. A source of air, nitrogen, or other transportgas(es) may be provided by gas source 171 to transport line 118 for thepurpose of entraining materials discharged from reservoirs 180 andinjecting such materials, via injection point 119, into flue gas stream15. Gas sources 170 and 171 may be the same or different, as desired.Alternatively, transport gas(es) may be provided to both transport lines115 and 118 by gas source 170 (connection from source 170 to line 118not shown). Although gas sources 170 and 171 are shown in FIG. 3 ascompressors or blowers, any source of transport energy known in the artmay be acceptable, as will be appreciated by those of skill in the art.

For clarity, single injection points 116 or 119 are shown in FIG. 3,although one skilled in the art will understand that multiple injectionpoints are within the scope of the present invention. Optical densitymeasuring device (s) 204 is connected to transport line 115 and/or 118to provide signals representative of the optical density insidetransport line 115 and/or 118 as a function of time.

Downstream from injection point 116 and 119 is provided particulateseparator 140. By way of illustration and not limitation, particulateseparator 140 may comprise one or more fabric filters, one or moreelectrostatic precipitators (hereinafter “ESP”), or other particulateremoval devices as are known in the art. It should be further noted thatmore than one particulate separator 140 may exist, sequentially or inparallel, and that injection point 116 and 119 may be at a locationupstream and/or downstream of 140 when parallel, sequential, orcombinations thereof exist. Particulate separator 140 produces at leasta predominantly gaseous (“clean”) stream 142, and a stream 141comprising separated solid materials. A sorbent/ash separator 150separates stream 141 into a largely ash stream 152, and a largelysorbent stream 151. Stream 151 may then preferably be passed to anoptional sorbent regenerator 160, which yields a regenerated sorbentstream 161 and a waste stream 162.

An optional Continuous Emission Monitor (hereinafter “CEM”) 205 formercury is provided in exhaust gas stream 35, to provide electricalsignals representative of the mercury concentration in exhaust stream 35as a function of time. The optional mercury CEM 205 and flow controllers201, 202, 203, 208, and 209 are electrically connected via optionallines 207 (or wirelessly) to an optional digital computer (orcontroller) 206, which receives and processes signals and preferablycontrols the preparation and injection of promoted carbon sorbent intocontaminated flue gas stream 15.

In operation, promoted carbon sorbent and/or an optional alkalicomponent is injected into contaminated flue gas stream 15. Aftercontacting the injected material with the contaminated flue gas stream15, the injected material reduces the mercury concentration,transforming contaminated flue gas into reduced mercury flue gas, 25.The injected material is removed from the flue gas 25, by separator 140,disposed of or further separated by optional separator 150, and disposedof or regenerated by an optional regenerator 160, respectively. Thereduced mercury “clean” flue gas stream 142 is then monitored formercury content by an optional CEM 205, which provides correspondingsignals to an optional computer/controller 206. Logic and optimizationsignals from 206 then adjust flow controllers 201, 202, 203, 208, 209 tomaintain the mercury concentration in exhaust stream 35 within desiredlimits, according to control algorithms well known in the art. Flowcontrollers 201, 202, 203, 208, 209 can also be adjusted manually or besome other automated means to maintain the mercury concentration inexhaust stream 35 within desired limits, according to control algorithmswell known in the art.

Referring still to FIG. 3, there are illustrated several preferredembodiments for preparation and injection of promoted carbon sorbentsand/or alkali components in accordance with the present invention.Stream 111 provides for introduction of base activated carbon fromreservoir 110, as metered by flow controller 201 manually or under thedirection of computer 206. The halogen/halide may be combined and reactwith the base activated carbon according to any of several providedmethods. The halogen/halide may preferably be combined via line 121directly into transport line 115, within which it contacts and reactswith the base activated carbon prior to injection point 116. This optionis one form of what is referred to herein as “in-flight” preparation ofa promoted carbon sorbent in accordance with the invention. Further, thehalogen/halide may be combined via line 121 b with base activated carbonprior to entering transport line 115. Still further, the halogen/halidemay be contacted and react with the base activated carbon byintroduction via line 121 c into reservoir 110. This option ispreferably employed when, for example, reservoir 110 comprises anebulliated or fluidized bed of base activated carbon, through whichhalogen/halide flows in gaseous form or as a vapor. Of course, thehalogen/halide may also preferably be contacted with the base activatedcarbon in liquid form or in a solvent, as discussed previously, andsolvent removal (not shown in FIG. 3) may then be provided if necessaryas mentioned with respect to embodiments discussed with reference toFIG. 1.

Similarly, the optional secondary component may be contacted and reactdirectly in transport line 115 via line 131, or optionally as describedabove with respect to the halogen/halide, via lines 131 b and 131 c.

Similarly, the optional alkali component from 180 may either be added intransport line 115 directly, or may be injected separately by transportline 118, combining downstream in flue gas 15 for synergistic effectswith base activated carbon, promoted carbon, or optional secondarycomponents. Being able to vary onsite the amount of the optional alkalicomponent relative to base activated carbon, promoted carbon, oroptional secondary components is a key feature to overcome and optimizefor site-specific operating and flue gas conditions.

In some preferred embodiments wherein contacting between components andreaction is performed in a liquid or solvent phase, stirring of suchliquid and/or slurry mixtures may be provided. In other embodiments, thehalogen/halide promoter and optional secondary component(s) maypreferably be sprayed in solution form into or on the base activatedcarbon. In some such embodiments, drying, filtering, centrifugation,settling, decantation, or other solvent removal methods as are known inthe art may then be provided.

In embodiments wherein the halogen/halide promoter is in gaseous orvapor form, it may be diluted in air, nitrogen, or other gas asappropriate. The halide/halogen gas, for example, gaseous HBr or Br₂,may be passed through an ebulliated or fluidized bed of granular orfibrous activated carbon, with the promoted carbon sorbent so producedremoved from the top of the bed via gas entrainment for injection.

In some embodiments, the secondary component(s) may preferably compriseiodine or other halogens, hydrohalides, including without limitation HI,HBr, HCl, a Group V or Group VI element with a molecular halogen, suchas SCl₂ and others. In some preferred embodiments, the promoted carbonsorbent may comprise from about 1 to about 30 g halogen/halide per 100 gbase activated carbon. In some preferred embodiments, the promotedcarbon sorbent may comprise an secondary component in concentration offrom about 1 to about 15 wt-% of the concentration of the halogen/halidecomponent.

In still other embodiments, the product promoted carbon sorbent may beapplied to a substrate. In other embodiments, such prepared substrate(s)may be caused to contact a contaminated flue gas or gasification systemproduct gas stream for mercury reduction purposes. Such substrates maybe monolithic, rotating, or exposed to the gas stream in any number ofways known to those skilled in the art.

In some embodiments, a method is provided whereby a mercury stabilizingreagent is added to a promoted carbon sorbent to produce a bifunctionalsorbent. Such stabilizing reagent(s) may be sequentially added, eitherbefore or after the addition and reaction of the halogen/halide. In somepreferred embodiments, the halogen/halide preferably comprises Br orHBr, and the mercury-stabilizing reagent may comprise S, Se, H₂S, SO₂,H₂Se, SeO₂, CS₂, P₂S₅, and combinations thereof.

Halogens in Mercury Capture

Methodologies for using halogens for the treatment of flue gas have beenproblematic, owing to their reactivity with other gases and metals,resulting in corrosion and health issues. A “halogen” is defined as amember of the very active elements comprising Group VITA (CASnomenclature is used throughout; Group VITA (CAS) corresponds to GroupVIIB (IUPAC)) of the periodic table. In the molecular elemental form ofthe halogens, including F₂, Cl₂, Br₂, and I₂, the reaction with a hotflue gas components leave little to react with elemental mercury. Theatomic elemental halogen form, which includes the fluorine, chlorine,bromine, and iodine atoms, is about a million times more reactive tomercury but the concentration of the atomic forms is typically extremelylow. In a large portion of electric utility coal combustion facilities,the concentrations are generally not sufficient to oxidize a significantamount of mercury.

The term “halide” as used herein is defined as a compound formed fromthe reaction of a halogen with another element or radical. In general,halide compounds are much less reactive than the molecular halogens,having a low chemical potential. Halides are considered reduced formsthat do not, alone, oxidize other compounds. In the conventional viewtherefore, a halide-salt-treated activated carbon will not effectivelyoxidize elemental mercury and capture elemental mercury.

Halogen Promoted Sorbent Characteristics

The sorbent described here has a very high initial reactivity foroxidizing mercury and therefore can be used in very small amounts toachieve very high capture efficiencies, thus lowering operation costsand lessening waste disposal problems. In addition, further disposalreductions are obtainable by regenerating and reusing the sorbentsproduced using the inventive technology. The time interval required forthe mercury and the promoted carbon sorbents of the present invention tosuccessfully interact in a flue gas duct, with the subsequent collectionof the mercury on the sorbent and ash is very short—less than seconds.Clearly, such collection times require the sorbent to have both highcapacity and high reactivity toward mercury. The promoted carbon sorbentcan be utilized in a very finely powdered form to minimize mass transferlimitations. However, again, the reactivity should be very high tocapture all of the mercury encountered by the fine particles.Additionally, use of these enhancement technologies allows capture to beeffective for larger sorbent particles which also allows separation ofthe sorbent from the ash to enable subsequent regeneration as well asash utilization. One feature of this invention is the process to preparea sorbent containing a halide compound formed on the carbon structurethat provides a sorbent that is highly active on initial contact withthe mercury contaminated gas stream, which allows for very effectivecapture of the mercury.

It appears that the inventive sorbents chemically combine molecularbromine, for example, from solution, with activated carbon (edge sites).X-ray photoelectron spectroscopy has established that the addition ofbromine, chlorine, HBr, or HCl formed a chemical compound in the carbonstructure. Thus, the sorbent produced from halogen and activated carbondoes not represent a molecular halogen form, but rather a new chemicallymodified carbon (or halocarbon) structure. This phenomenon may not occurwith the less reactive iodine, where an I₂ molecular complex can existon the carbon basal plane. In the case of bromine, modified cationiccarbon has a high chemical potential for oxidation of mercury. Thus, anentirely new model is presented for the reactivity of thebromine-treated carbon with mercury. The reactive carbon form canpreferably be generated by the addition of bromine, hydrogen bromide, orcombinations of bromine and other elements, as described herein. Halogentreatment resulted in higher-activity carbons because the halide anions(especially bromide and iodide) were effective in promoting theoxidation by stabilizing the developing positive charge on the mercuryin the transition state for oxidation. Based on this model, severalinnovative, inexpensive, activity-enhancing features have beendeveloped.

Optional Second Component

It has been demonstrated that addition of an optional second component,in addition to the bromine, results in improved reactivity and capacityfor the sorbent, typically exceeding that of both the untreated carbonand the brominated carbon. The second compound comprises either a secondhalogen or a compound derived from a second halogen, such as HI. Thus,in addition to having a reactive carbon form present, the secondcomponent generates a Lewis base with greater ability to stabilize thedeveloping positive charge on the mercury. Thus, the second component isan element with more polarized electrons (4 p and 5 p).

Optional Alkali Component

It has been demonstrated that addition of an optional alkali componentwith a base or promoted activated carbon results in improved mercurycapture, typically exceeding that of both the untreated carbon and thepromoted carbon. Test data indicate that flue gas contaminants, flue gasconstituents (SO₂, NO_(x), HCl, etc), operating temperature, mercuryform, and mercury concentration may impact the effectiveness of thealkali addition. This suggests the need to be able to adjust and tailorthe alkali-to-activated-carbon ratio onsite in order to overcome andoptimize for a given set of site conditions.

The synergy that can be gained when co-injecting the two materials canbe explained as follows. First, testing shows that binding sites onactivated carbon (hereinafter “AC”) can be consumed by chlorine species,sulfur species (i.e. sulfates), and other flue gas contaminants(arsenates, selenates, etc). The addition of optional alkali materialwill interact and react with these species/contaminants thus minimizingtheir consumption of AC mercury binding sites. Second, testing alsoshows that standard AC will continue to oxidize mercury, even though thebinding sites are fully consumed. This oxidized mercury can then reactwith alkali material and subsequently be captured by particulate controldevices. Consequently, the addition of the optional alkali componentacts to protect mercury binding sites and capture oxidized mercury,thereby resulting in improved mercury reduction at lower cost. Alkali isgenerally much lower in cost (˜an order of magnitude less) thanactivated carbon, thus more of it can be used still resulting in overalllower costs.

“In-Flight” Sorbent Preparation

Furthermore, we have demonstrated that the halogen promoted carbonsorbent can be readily produced “in-flight”. This is accomplished by,for example, contacting the vapors of any combination of halogens andoptionally a second component, in-flight, with very fine carbonparticles. The particles may be dispersed in a stream of transport air(or other gas), which also conveys the halogen/halide promoted carbonsorbent particles to the flue gas duct, or other contaminated gasstream, from which mercury is to then be removed. There is no particulartemperature requirement for this contact. This technology is obviouslyvery simple to implement, and results in a great cost savings tofacilities using this technology for mercury capture.

Advantages of On-Site Preparation

In-flight preparation of the halogen/halide promoted carbon sorbent onlocation produces certain advantages. For example, the treatment systemcan be combined with the carbon injection system at the end-use site.With this technique, the halogen/halide is introduced to the carbon-air(or other gas) mixture in a transport line (or other part of the sorbentstorage and injection system). This provides the following benefits overcurrent conventional concepts for treating sorbents off-site:

-   -   Capital equipment costs at a treatment facility are eliminated.    -   Costs to operate the treatment facility are eliminated.    -   There are no costs for transporting carbon and additive to a        treatment facility.    -   The inventive process uses existing hardware and operation        procedures.    -   The inventive technology ensures that the sorbent is always        fresh, and thus, more reactive.    -   No new handling concerns are introduced.    -   There are no costs for removing carbon from treatment system.    -   The inventive process allows rapid on-site tailoring of        additive-sorbent ratios in order to match the requirements of        flue gas changes, such as may be needed when changing fuels or        reducing loads, thus further optimizing the economics.    -   The inventive technology reduces the amount of spent sorbents        that are disposed.

With the foregoing and other features in view, there is provided, inaccordance with the present invention, embodiments including a processfor preparing and regenerating halogen/halide promoted carbon sorbents,whose activity for mercury capture is enhanced by the addition ofhalogen (e.g. bromine) to the carbon structure.

Sorbent Injection Location

Some of the preferred embodiments contemplate the use of a halogenpromoted sorbent in a powdered form that has been injected into a fluegas stream before or after ash particulates have been removed. Otherembodiments of the inventive composition of the halogen promoted carbonsorbent comprise a powdered modified activated carbon prepared by addingBr₂ or HBr plus a second optional component. Other embodiments allow theaddition of the optional alkali component in conjunction with a baseactivated carbon and/or with the use of a halogen based sorbent and anyother combinations of the sorbent technologies provided in this patent.Alternatively, embodiments include methods wherein the sorbent is on amoving contactor consisting of particles or fibers containing one ormore of the compositions listed above.

Sorbent Regeneration

Any of the above embodiments of the halogen/halide promoted carbonsorbent can be easily regenerated; the poisoning contaminants from theflue gas are preferably removed and an inexpensive promoting agentadded, to restore mercury sorption activity. This process of promotingthe activity of the carbon itself contrasts with the earlier, moreexpensive, conventional methods of adding a reagent (such as peroxide,gold, triiodide, etc.) to a sorbent. The halogen/halide promoted carbonsorbent of the present invention, treated with bromine and/or optionalcomponents, is noncorrosive. Detailed examples of sorbent regenerationtechniques are described in co-pending, commonly owned PCT patentapplication No. PCT/US04/12828, titled “PROCESS FOR REGENERATING A SPENTSORBENT”, which is hereby incorporated by reference in its entirety.

Sorbent Injection Control Schemes

Another advantage of the present invention relates to the use of afeedback system to more efficiently utilize certain aspects of theinvention. Where possible and desirable, the mercury control technologyof the present invention may preferably utilize continuous measurementof mercury emissions as feedback to assist in control of the sorbentinjection rate. Tighter control on the sorbent and optional component(s)levels can be achieved in this way, which will ensure mercury removalrequirements are met with minimal material requirements, thus minimizingthe associated costs. In an embodiment, the mercury emissions arecontinuously measured downstream of the injection location, preferablyin the exhaust gas at the stack.

Promoted Carbon Sorbents

Reactions of halogens and acidic species with the basic binding sites onthe activated carbon sorbent create sites for oxidizing mercury. Othermetal ions, such as boron, tin, arsenic, gallium, Sb, Pb, Bi, Cd, Ag,Cu, Zn, or other contaminants, will also react with the oxidation sitesgenerated on the carbon.

According to our model, adding the bromine from the bromine reagent or aproton from a hydrogen halide acid to a basic carbene site on the carbonedge structure forms a carbocation that accepts electrons from theneutral mercury atom forming the oxidized mercury species that is boundto the sorbent surface. The reactive site may also generate reactivebromine radicals or carbon radicals at the active sites on the carbon.Thus, the activated carbon serves to stabilize the bromine, yet providesa highly reactive bromine-containing reagent that can oxidize themercury and promote its capture on the activated carbon. The sorbentthat contains bromine is expected to be more reactive than thecorresponding sorbent containing chlorine and much less expensive thanthe sorbent containing iodine.

EXAMPLES

To more clearly illustrate the present invention, several examples arepresented below. These examples are intended to be illustrative and nolimitations to the present invention should be drawn or inferred fromthe examples presented herein.

Example 1 Preparation and Testing of Halogenated Carbon (& ComparativeExample)

Gas Phase Halogenation

Finely powdered activated carbon (such as NORIT Darco FGD, NORITAmericas, Inc., Marshall, Tex. (USA), although others are suitable, aswill be recognized by those skilled in the art), was placed in arotating plastic barrel with side blades (a 5 ft³ (0.14 m³) cementmixer) fitted with a tight plastic lid to prevent loss of the finepowder during the preparation. In a separate vessel, gas phase brominewas generated by passing a nitrogen stream over a weighed amount ofliquid bromine that is warmed to about 40°-50° C. The vapor pressure ofthe bromine was such that a dark red gas is generated and passed out ofthe generator. The outlet from the gaseous bromine generator isconnected via a ¼ inch (0.64 cm) plastic hose to a stationary metal tubeinserted through a flange in the center of the plastic lid and passinginto the center of the barrel. The flange is not air tight so that theexcess of nitrogen is released after the bromine is transferred to thetumbling carbon. Thus, the bromine gas stream continuously passed intothe rotating barrel where it contacted the tumbling carbon. The unit isthen operated until the desired amount of bromine has combined with thecarbon. Typically, this is 0.4 to 1 kg of bromine to 20 kg of carbon(2-5 wt. %). When the reaction is completed, the carbon is weighed. Thetreated carbon is odorless and does not cause skin irritation since thebromine has completely reacted with the carbon to produce the brominatedcarbon.

XPS spectra demonstrate that the brominated carbon contains bothcovalent carbon-bound (organic) bromide as well as anionic bromide. Theproduct contains the same moisture originally present in the activatedcarbon (5-17 wt %), but does not require further drying for use. Themoisture is driven out at higher temperatures (>150° C.), and thebromine was not released until very high temperatures

Bench-Scale Testing of Mercury Oxidation and Capture Efficiency

A bench-scale apparatus and procedure based on the above description wasused to test the initial activities and capacities of several promotedactivated carbon sorbents using powdered carbon, includingbromine-containing activated carbons prepared from a variety of carbons,including commercially available sorbents, aerogel film sorbents, andthe original precursor carbons for comparison.

A detailed description of the apparatus and its operation is provided inDunham, G. E.; Miller, S. J. Chang, R.; Bergman, P. EnvironmentalProgress 1998, 17, 203, which is incorporated herein by reference in itsentirety. The bench scale mercury sorbent tests in the flue gascompositions were performed with finely (−400 mesh) powdered sorbents(37 mg) mixed with 113 mg sand and loaded on a quartz filter (2.5 inch(6.35 cm)). The loaded filter and holder were heated in an oven (125°C.) in the simulated flue gas stream (30 SCFH (standard cubic feet/hr)or 0.79 NCMH (normal cubic meters per hour)) containing the following:O₂ (6%), CO₂ (12%), SO₂ (600 ppm), NO (120 ppm) NO₂ (6 ppm), HCl (1ppm), Hg⁰ (11 μg/m³), H₂O (15%), and N₂ (balance). Elemental mercury wasprovided by a standard permeation tube source placed in a doublejacketed glass condenser, and heated to the desired temperature. Mercuryconcentrations in the gas streams were determined with a continuousmercury emission monitor (Sir Galahad mercury CEM mfr. P.S. AnalyticalDeerfield Beach Fla. USA), and a SnCl₂ cell was used to convert oxidizedspecies to elemental, so that both elemental and oxidized mercuryconcentration data could be obtained for both the influent and theeffluent concentrations from the sorbent bed. Mercury concentrationswere calibrated for the flow rates used. Spent sorbents were analyzedfor mercury to determine the mass balance.

Referring now to FIG. 4, the effluent mercury concentration data areplotted as a percent of the influent mercury versus time. The resultingcurve (breakthrough curve) for the halogenated sorbents typically showed0%-1% Hg in the effluent (99+% capture) at the beginning, and increasingonly after 30-60 minutes (breakthrough point), depending on the sorbent.FIG. 4 illustrates the breakthrough curves for 5 wt/wt % brominatedNORIT Darco FGD sorbent (37 mg+113 mg sand) with synthetic flue gascontaining 1 ppm HCl. Total Hg (solid circles) and elemental Hg (solidsquares) in the effluent are presented as a per cent of the inlet Hg.“EOT” indicates the end of test (the later data points shown are forcalibration checks).

FIG. 5 presents the comparative breakthrough curves for thecorresponding nonhalogenated sorbents typically initiated at 5%-50% ofinlet mercury, depending on the HCl concentration in the synthetic fluegas, thus indicating considerably lower reactivity for oxidation andcapture of the mercury for the nonhalogenated sorbents. Afterbreakthrough of either halogenated or nonhalogenated sorbent, most ofthe mercury in the effluent was oxidized mercury.

Example 2 Gas Phase Halogenation of Fluidized Carbon

A bed of activated carbon supported in a vertical tube by a plug ofglass wool was fluidized by a nitrogen stream. The top of the fluidizedbed tube was connected to a catching trap for carbon fines that blow outthe top of the tube. The bromine gas generator as described in Example 1was attached to the fluidized carbon bed and the desired amount ofgaseous bromine was passed into the bed. The contents of the trap werethen mixed with the material in the bed and weighed. The resultingbrominated carbon exhibited properties similar to the brominated carbonof Example 1.

Example 3 Liquid Phase (water) Halogenation

A 5% solution of bromine in water was prepared by carefully adding 50 gof bromine to 1 liter of cold water. One kg of activated carbon wasadded to the bromine solution in a large metal can. The resulting slurrywas stirred with a large paddle during the addition and for a short timeafterwards until all the bromine had reacted with the carbon, asindicated by the disappearance of the red color. The slurry was thenfiltered using a Buchner funnel under vacuum. The moist carbon that wascollected on the filter was dried in an oven at 110° C. for severalhours to constant weight. As in Example 1, some moisture remains in thecarbon, however. The dried carbon was then tumbled in the rotatingbarrel with metal pieces to break up and fluff the carbon.

Example 4 Addition of the Optional Second Halide Component

Brominated carbon was produced by solution phase bromination similar tothat described with reference to Example 3. However, before filtration,a solution of hydriodic acid (HI) was added to the slurry in an amountequal to 10% of the bromine amount. The slurry was stirred to completethe reaction and then filtered and dried as described in Example 3.

Example 5 Liquid Phase Phosphohalogenation

A solution of phosphorus tribromide (500 g) in ligroin (10 liters) wasstirred in a large metal can and 10 kg of activated carbon was added.The resulting slurry was stirred with a large paddle at ambienttemperature to complete the reaction. The slurry was filtered undervacuum on a large Buchner funnel in several batches. The wet filter cakewas dried at 110° C. in an oven to constant weight. The dried productwas fluffed in the rotating barrel as described in Example 3.

Example 6 Preparation and Sorption on Larger-Particle Carbon

Tests were conducted on a pilot-scale combustor while firing asubbituminous coal, to evaluate mercury control by injectinglarger-than-normal sized treated activated carbon. Standard AC sorbentsgenerally are of fine size with a mean particle diameter of less than 20micrometers, which is also typical of the flyash that is generated frompulverized coal combustion. Consequently, because the sizes of standardAC and flyash are similar, separation of the two is difficult. Injectionof larger sized AC is generally not considered because the sorbenteffectiveness decreases with size. In a scheme to recycle the injectedcarbon, the carbon is separated from the flyash. A separation based onsize fractionation requires a treated larger particle sorbent. To testthis concept, a treated larger sized (>60 μm) sorbent was developed,prepared, and tested.

Treatment—Gas Phase Halogenation

Granular activated carbon (Calgon F400) was ground and sieved throughconventional mesh screens. The mesh size fraction −170 to +240(corresponding to about 60 to about 88 micrometers) was collected andplaced in a rotating vessel as described in Example 1 above. In aseparate vessel, gas phase bromine was generated by passing a nitrogenstream over a weighed amount of liquid bromine that was warmed to about40°-50° C., and the outlet from this gaseous bromine generator wasconnected via a ¼ inch (6.35 mm) plastic hose to a stationary metal tubeinserted through a flange in the center of the lid and passing into thecenter of the rotating vessel, also as described in Example 1. The unitwas operated until the desired amount of bromine had combined with thecarbon, in this case 0.05 kg of bromine to 1 kg of carbon (5 wt. %).When the reaction was completed, the carbon was weighed. The treatedcarbon was odorless as has been described above.

PTC Apparatus

The pilot-scale combustor, known as the “Particulate Test Combustor”(hereinafter “PTC”), is a 550,000-Btu/hr (about 161 kW) pulverized coal(“PC”)-fired unit, designed to generate combustion flue gas propertiesand fly ash that are representative of those produced in a full-scaleutility boiler. The combustor is oriented vertically to minimize walldeposits. A refractory lining helps to ensure adequate flame temperaturefor complete combustion and prevents rapid quenching of the coalescingor condensing fly ash. Based on the superficial gas velocity, the meanresidence time of a particle in the combustor is approximately 3seconds. The coal nozzle of the PTC fires axially upward from the bottomof the combustor, and secondary air is introduced concentrically to theprimary air with turbulent mixing. Coal is introduced to the primary airstream via a screw feeder and eductor. An electric air preheater is usedfor precise control of the combustion air temperature. Originally, thePTC used cold-water annular heat exchangers to provide flue gastemperature control to the baghouse (also referred to as a “fabricfilter”) or electrostatic precipitator (ESP). However, analysis of ashdeposits collected from the heat exchangers indicated that some mercurywas collected on the duct walls. To minimize this effect, the heatexchangers were modified to provide for higher duct wall temperatures.

The PTC instrumentation permits system temperatures, pressures, flowrates, flue gas constituent concentrations, and particulate controldevice (baghouse, Advanced Hybrid Particle Collector/AHPC™, and/orelectrostatic precipitator/ESP) operating data to be monitoredcontinuously and recorded on a data logger.

PTC Procedure

Flue gas samples were taken at combinations of two of the threeavailable system sample points: the furnace exit, the particulatecontrol device inlet, and the particulate control device outlet. Afterpassing through sample conditioners to remove moisture, the flue gas wastypically analyzed for O₂, CO, CO₂, SO₂, and NO_(x). Each constituentwas normally analyzed at both the furnace exit and the outlet of theparticulate control device simultaneously, using two analyzers. Theconcentration values from all of the instruments were recordedcontinuously. In addition, data were manually recorded at set timeintervals. NO was determined using a pair of Rosemount Analytical NOchemiluminescent analyzers. SO₂ was measured using a pair of AmetekInstruments photometric gas analyzers. The remaining gases were measuredby a pair of Rosemount Analytical multi-gas continuous emissionsmonitors. Each of these analyzers was regularly calibrated andmaintained to provide accurate flue gas concentration measurements.

The baghouse vessel was a 20 inch (50.8 cm) (ID) chamber that isheat-traced and insulated, with the flue gas introduced near the bottom.The combustor produced about 200 ACFM (actual cubic feet per minute;about 5.7 actual m³/min) of flue gas at 300° F. (about 150° C.),therefore three 13-ft by 5-inch (3.96 m by 12.7 cm) bags provided anair-to-cloth ratio of 4 ft/min (1.22 m/min). Each bag was cleanedseparately in operation with its own diaphragm pulse valve. In order toquantify differences in pressure drop for different test conditions, thebags were cleaned on a time basis, rather than with the cleaning cycleinitiated by pressure drop. Once bag cleaning was initiated, all threebags were pulsed in rapid succession on-line.

Tests were also conducted with a single-wire, tubular ESP replacing thefabric filter. The ESP unit was designed to provide a specificcollection area of 125 at 300° F. (150° C.). Since the flue gas flowrate for the PTC is 130 SCFM (standard cubic feet per minute; about 3.7NCMM (normal m³/min)), the gas velocity through the ESP is 5 ft/min(about 1.52 m/min). The plate spacing for the ESP unit is 11 in (27.9cm). The ESP was designed to facilitate thorough cleaning between testsso that all tests can begin on the same basis.

PTC Results

Results are illustrated in FIG. 6. As can be observed in FIG. 6, eventhough the tested sorbent particle size is significantly larger thannormal sorbent particles, the treated larger-than-normal sized (thatis, >60 micrometers) activated carbon sorbent was quite effective atcapturing mercury. Approximately 75% of the mercury was captured whenthe larger-sized treated AC was injected ahead of the pilot-scale ESP,while approximately 85% of the mercury was captured when injected aheadof the pilot-scale fabric filter (“FF”). Note that in FIG. 6 (andthroughout) “Macf” (and “MACF”) indicates million actual cubic feet (1MACF is about 0.028 million actual cubic meters or “MACM”).

Referring now to FIG. 7, it can be observed that the larger-sizedtreated AC when injected ahead of the pilot-scale ESP (diamondsymbol(s)) performed better than the finer standard AC (triangles) underthe same arrangement. In comparison, when injected ahead of the fabricfilter (FF), the larger-sized treated AC (square) performed similarly toslightly worse. However, for this application, the larger-sized treatedAC can be physically separated from the smaller flyash particles, andthe sorbent can then be regenerated, recycled, and reused. This willsubstantially improve overall utilization and economics. These data thusshow that a larger-than-normal sized sorbent can provide effectivemercury control and ease flyash and AC separation, thereby alsopreserving the characteristics of the flyash for sale and beneficialuse. Accordingly, because >60 μm sorbent particles have beensuccessfully demonstrated, superior mercury control can be obtainedwith >40 μm particles, which may be preferred in some applications,depending on the sorbent particle/ash separation system used. Note thatin FIG. 7 (and throughout) “Macf” (and “MACF”) indicates million actualcubic feet.

Example 7 Liquid Phase (Organic Solvent) Halogenation

A 5% solution of bromine in ligroin was prepared by carefully adding 50g of bromine to 1 liter of cold ligroin. One kg of activated carbon wasadded to the bromine solution in a large metal can. The slurry wasstirred with a large paddle during the addition and for a short timeafterwards until all the bromine had reacted with the carbon asindicated by the disappearance of the red color. The slurry was filteredusing a Buchner funnel under vacuum. The carbon cake that was collectedon the filter was dried in an oven at 110° C. for several hours until itappeared dry and a constant weight was obtained. As in Example 1, somemoisture was left in the carbon, however. The dried carbon was thentumbled in the rotating barrel with metal pieces to break up and fluffthe carbon.

Example 8 Promoted Activated Carbon Sorbents

A bench-scale procedure based on the above description was used to testthe initial activities and capacities of several promoted activatedcarbon sorbents using powdered carbon, including the bromine-containingactivated carbons prepared from a commercially available sorbent and anaerogel carbon film sorbent, as well as the original precursor carbonsfor comparison. Bromine-treated carbons were prepared by impregnation ofthe powdered activated carbon precursors in a stirred solution ofbromine in carbon tetrachloride or methylene chloride, or alternatively,in an aqueous solution of HBr, followed by drying in air at ambienttemperature and drying in an oven at 100° C. in air or nitrogen.Bromine-treated carbons were also prepared by impregnating bromine fromthe gas phase by passing the gas through a rotating dry bed of theactivated carbon precursor. The results indicated that adding a secondcomponent to the solution improved the capacity of the sorbent.

The carbons were initially tested in a heated bed, where a syntheticflue gas stream containing elemental mercury (11 μg/m³) was passedthrough the bed. Concentrations of total and elemental Hg in theeffluent gas were determined using a Sir Galahad mercury CEM(“continuous emission monitor”) (mfr. P S Analytical, Deerfield Beach,Fla., USA). The powdered sorbent was supported on a quartz filter duringthe test, and the other sorbents were tested as a triple layer. Acomparison of the original commercial-grade powdered carbon sorbent withthe sorbent after it was treated with 0.1 N HBr, and the powder wascollected by centrifugation and drying, revealed that the mercurycapture activity increased from an initial capture efficiency of about50% of the Hg in the inlet to 100% capture. A comparison of the sorbentafter subsequent regeneration with HBr indicated that it not onlycaptured mercury at the same level as before (100% capture) but itscapacity was prolonged by several minutes, and thus enhanced. Similarresults were obtained with the carbon film and carbon fiber sorbents bytreatment with molecular bromine in solution or in dry beds as describedabove.

Example 9 Fluidized/Ebulliated Bed Preparation

An activated carbon sorbent was prepared by treating the carbon byimpregnating molecular bromine from a gas composition containingmolecular bromine by flowing the gas through a liquid bromine reservoirin series with a fluidized bed or ebulliated bed of the carbon. Theamount of bromine taken up by the carbon ranges (in one example) from <1to about 30 g per 100 g of activated carbon, depending on theproportions used.

Example 10 Full-Scale Testing

In this example, a baghouse (fabric filter) or ESP was used to collectparticulates in the exhaust of a full-scale commercial pulverizedcoal-burning facility. A scrubber and sorbent bed were also used toremove undesired constituents from the flue gas stream, before being fedto the stack. In this example, the halogen/halide promoted carbonsorbent was injected into the flue gas after the boiler. In generalhowever, the inventive sorbent can be injected where desired (e.g.,before, after, or within the boiler).

In one exemplary test conducted at a facility fired with lignite coal,the flue gas phase mercury (elemental) concentration was between 10 and11 μg/m³. The ash and injected carbon were collected in the baghouse at350° F. to 375° F. (about 175-190° C.). Injection of commercial-gradeactivated carbon powder (untreated) at a rate of 1.0 lb/MACF (“MACF” and“Macf” represent one million actual cubic feet; 1.0 lb/MACF is about 16kg/MACM (million actual cubic meters)) resulted in mercury effluentconcentrations of 3.8-4.2 μg/m³ (representing 62%-58% removal of themercury from the gas, respectively), and at 2.0 lb/MACF (about 32kg/MACM), gave 74%-71% removal. Injection of the bromine-treated carbonat 1.0 lb/MACF resulted in 73%-69% removal and at 2.0 lb/MACF gave86%-84% removal. Thus, a significant increase in the mercury capture wasexhibited during use of the bromine promoted carbon sorbent of thepresent invention.

Example 11A Addition of Optional Alkaline Component—Bench-Scale

The efficiency of the activated carbons for mercury capture can beimproved considerably by employing a basic material co-injected with theactivated carbon, in order to capture any oxidized mercury that may bereleased from the sorbent, or to capture some of the sulfur or seleniumoxides in the flue gas that can have a detrimental effect on the sorbentcapacity.

Bench-scale testing was conducted by preparing a filter composed of 37mg of brominated activated carbon mixed with 113 mg of calcium oxide.The test was conducted as described in Example 1 and compared with thesame carbon sorbent but with an inert diluent. The breakthrough curvefor the mixture of brominated (2%) NORIT Darco FGD sorbent with inertsand is shown in FIG. 8, and the breakthrough curve for the mixture withCaO is shown in FIG. 9. It can be seen that the point of 50%breakthrough improves to 65 minutes with the mixture with CaO from only48 min with the sand mixture.

Example 11B Addition of Optional Alkaline Component—Pilot-Scale

Tests were conducted on the pilot-scale PTC combustor described abovewith reference to Example 6 while firing a Texas lignite to evaluatemercury control by co-injecting a standard activated carbon (alsoreferred to herein as “AC”) and an alkali material upstream of a fabricfilter. Typical results are illustrated in FIG. 10. As shown in FIG. 10,co-injecting lime with activated carbon vastly improved mercury removal.Mercury removals of approximately 90% were achieved with the co-injectedsorbents, whereas less than 60% removal was achieved with the use ofstandard AC alone, even at much higher injection rates. Data fromsimilar tests show that injecting similar quantities of sodium carbonateand AC, and lime and AC, resulted in mercury removals of approximately80%, and 87%, respectively. These data suggest that other alkali canalso be co-injected with AC to improve mercury removal. Other data showthat flue gas temperature may impact the effectiveness of the alkaliaddition. Further test data indicate that flue gas contaminants, fluegas constituents (SO₂, NO_(x), HCl, etc.), operating temperature,mercury form, and mercury concentration may impact the effectiveness ofthe alkali addition. This indicates that it may be desirable to be ableto adjust and tailor, onsite, the alkali-to-AC ratio in order tooptimize removal for a given set of site conditions.

Without wishing to be bound by any particular theory, the synergyobserved in the improved performance when co-injecting the two materialscan be explained as follows. First, tests indicate that binding sites onAC can be consumed by sulfur species and other contaminants. The alkalimaterial interacts and reacts with these species thus minimizing theirconsumption of AC mercury binding sites. Second, other work has shownthat standard AC will continue to oxidize mercury even though thebinding sites are fully consumed. This oxidized mercury can then reactwith alkali material and subsequently be captured by the particulatecontrol device. Thus, combining alkali with treated and/or non-treatedAC synergistically takes advantage of these two mechanisms, resulting inimproved mercury capture at reduced costs.

Example 12 Brominated Carbon Sorbent for Gasification Fuel GasPreparation of 5% Br2W-AC

Using a procedure similar to Example 3, a 2.5 wt/vol % solution ofbromine in water was prepared. Granular Calgon F400 was added to thebromine solution to give a 5 wt/wt % brominated carbon product. Thebromine solution was stirred with a large paddle during and after theaddition until the red color in the water disappeared. The suspensionwas filtered by vacuum on a large Buchner funnel. The filter cake wasdried in air, and then in an oven at 110° C. until a stable weight wasobtained The moisture was reduced to 15%.

Preparation of 5% Br2D-AC

A brominated sorbent was prepared from Br₂ addition in solvent asdescribed in Example 7, except that dichloromethane was used as thesolvent instead of ligroin, and granular Calgon F400 was used.

Preparation of 5% PBr3-AC

A phosphohalogenated sorbent was prepared from PBr₃ using the methoddescribed in Example 5, except granular Calgon F400 was used.

Testing in Hydrogen Atmosphere—Procedure

To simulate the capture of mercury from a heated fuel gas or syngas fromcoal gasification, tests were conducted employing a stream comprising10% vol/vol hydrogen in nitrogen passing through the sorbent at 500cc/min. The stream contained 26.9 micrograms/m³ of elemental mercuryfrom a commercial mercury permeation source.

In the tests, the sorbent (0.5 g) was placed in a 0.39 inch (1 cm,inside diameter) glass tube fitted with a medium frit sintered glassfilter disc to hold the sorbent in the gas stream. The tube containingthe sorbent bed was connected to a gas inlet tube for introducing thegas stream containing the mercury vapor and at the outlet to a tubeconnection to the detector. The detector was a Semtech 2000 continuousmercury emission monitor. The tube was equilibrated in a nitrogen flow(450 cc/min) for 5 minutes at ambient temperature to stabilize thesystem. The detector showed 0 concentration of mercury in the effluentfrom the sorbent bed. (The blank run with no sorbent read 26.9micrograms/m³). The tube was then placed in an oven at the selectedtemperature for the test (from 250° to 400° C.). Effluent mercuryconcentration data from the detector were collected until the detectorshowed a constant reading for 5 minutes. Hydrogen (50 cc/min) was thenadded to the gas stream and detector readings were taken every 5 min.Tests were conducted at several oven temperatures for various periods oftime up to 3 hours, depending on the temperature and sorbent. Theelemental mercury concentration data were plotted as a percent of inletmercury concentration versus time as in Example 1. All the mercury inthe effluent was elemental, so a single detector was sufficient, and noSnCl₂ trap was needed to convert to elemental mercury (as in Example 1).The time for 50% breakthrough (time to reach 50% capture) was thendetermined from the breakthrough curves.

Results

The results are shown in Table 1 (below) for the unbrominated sorbent(Calgon F-400), the brominated sorbents (5% Br2W-AC and 5% BrD-AC), andthe phosphobrominated sorbent (5% PBr3-AC). The maximum mercuryconcentration obtained in the effluent in each run is also reported inTable 1 for the time period indicated in the last column.

Under the reducing hydrogen conditions, the unbrominated sorbent brokethrough immediately and was exhausted after only 6.5 min. This completefailure occurred because the hydrogen reduces the captured mercury inthe unbrominated sorbent at any temperature above 100° C. Both of thebrominated sorbents exhibited excellent reactivity and good capacity atall temperatures, up to at least 400° C. The phosphobrominated sorbentexhibited superior reactivity and capacity at all temperatures, up to atleast 400° C.

TABLE 1 Times for 50% Breakthrough Maximum Observed Hg Concentrationsfor Sorbents (10% Hydrogen Streams) Temp 50% breakthrough Maximum [Hg]Time Sorbent (° C.) (min) (μg/m³) (min) F-400 250 6 20.3 6.5 5%Br2W-AC250 >150 1.4 150 5%Br2W -AC 300 >180 4.3 180 5%Br2W-AC 350 160 15.1 1805%Br2W-AC 400 60 13.9 65 5%PBr3-AC 250 >140 0.4 140 5%PBr3-AC 300 >1500.5 150 5%PBr3-AC 350 >150 1.4 150 5%Br2D-AC 350 >180 2.1 180 5%Br2D-AC400 >180 10.9 180

While the preferred embodiments of the invention have been shown anddescribed, modifications thereof can be made by one skilled in the artwithout departing from the spirit and teachings of the invention. Theembodiments described herein are exemplary only, and are not intended tobe limiting. Many variations and modifications of the inventiondisclosed herein are possible and are within the scope of the invention.Accordingly, the scope of protection is not limited by the descriptionset out above, but is only limited by the claims which follow, thatscope including all equivalents of the subject matter of the claims.

The examples provided in the disclosure are presented for illustrationand explanation purposes only and are not intended to limit the claimsor embodiment of this invention. While the preferred embodiments of theinvention have been shown and described, modifications thereof can bemade by one skilled in the art without departing from the spirit andteachings of the invention. Process criteria, equipment, and the likefor any given implementation of the invention will be readilyascertainable to one of skill in the art based upon the disclosureherein. The embodiments described herein are exemplary only, and are notintended to be limiting. Many variations and modifications of theinvention disclosed herein are possible and are within the scope of theinvention. Use of the term “optionally” with respect to any element ofthe invention is intended to mean that the subject element is required,or alternatively, is not required. Both alternatives are intended to bewithin the scope of the invention.

The discussion of a reference in the Background is not an admission thatit is prior art to the present invention, especially any reference thatmay have a publication date after the priority date of this application.The disclosures of all patents, patent applications, and publicationscited herein are hereby incorporated herein by reference in theirentirety, to the extent that they provide exemplary, procedural, orother details supplementary to those set forth herein.

Although the invention is described herein as a sorbent material andassociated processes for its preparation and use, it is nevertheless notintended to be limited to the details described, since variousmodifications and structural changes may be made therein withoutdeparting from the spirit of the invention and within the scope andrange of equivalents of the claims.

1. (canceled)
 2. A method for separating mercury in a gas stream comprising: contacting carbon including at least some graphene and a promoter selected from the group consisting of an elemental halogen, a group V halide, a group VI halide, a hydrohalide, and combinations thereof, to form a promoted sorbent particulate; modifying at least some edge structures of at least some of the graphene of the carbon for forming carbocations for the promoted sorbent for accepting at least some electrons from mercury atoms of the mercury; and contacting the mercury-containing gas stream and the promoted sorbent particulate for forming a stabilized mercury-sorbent particulate from the gas stream.
 3. The method of claim 2, wherein the promoter is an elemental halogen or a hydrohalide, or a combination.
 4. The method of claim 3 wherein the elemental halogen is bromine, or wherein the hydrohalide is hydrogen bromide, or both.
 5. The method of claim 2, wherein the promoter is a group V halide or a group VI halide.
 6. The method of claim 5 wherein the promoter is PBr₃ or SCl₂.
 7. The method of claim 2 further comprising contacting the promoted sorbent particulate, the mercury-containing gas stream, or both, with an alkaline material.
 8. The method of claim 2, wherein the promoter is in gaseous form.
 9. The method of claim 2, wherein the promoter is in an organic solvent.
 10. The method of claim 9, wherein the organic solvent is a hydrocarbon, a chlorinated hydrocarbon, or supercritical carbon dioxide.
 11. The method of claim 2, wherein the mercury-containing gas stream is a product of coal or petroleum combustion.
 12. A method for separating mercury in a gas stream comprising: contacting carbon including at least some graphene and a promoter including at least one of bromine, bromine compounds, and combinations thereof to form a promoted sorbent particulate; modifying at least some edge structures of the graphene for forming carbocations for accepting some electrons from mercury atoms of the mercury; and contacting the mercury-containing gas stream and the a promoted sorbent particulate for forming a stabilized mercury-sorbent particulate from the gas stream.
 13. The method of claim 12, wherein the promoter is an elemental halogen or a hydrohalide, or a combination.
 14. The method of claim 13 wherein the elemental halogen is bromine, or wherein the hydrohalide is hydrogen bromide, or both.
 15. The method of claim 12, wherein the promoter is a group V halide or a group VI halide.
 16. The method of claim 15 wherein the promoter is PBr₃ or SBr₂.
 17. The method of claim 12 further comprising contacting the promoted sorbent particulate, the mercury-containing gas stream, or both, with an alkaline material.
 18. The method of claim 12, wherein the promoter is in gaseous form.
 19. The method of claim 12, wherein the promoter is in an organic solvent.
 20. The method of claim 19, wherein the organic solvent is a hydrocarbon, a chlorinated hydrocarbon, or supercritical carbon dioxide.
 21. The method of claim 12, wherein the mercury-containing gas stream is a product of coal or petroleum combustion. 